CN101117585B - Industrialized method for producing fuel oil by using waste plastics - Google Patents
Industrialized method for producing fuel oil by using waste plastics Download PDFInfo
- Publication number
- CN101117585B CN101117585B CN200710153837XA CN200710153837A CN101117585B CN 101117585 B CN101117585 B CN 101117585B CN 200710153837X A CN200710153837X A CN 200710153837XA CN 200710153837 A CN200710153837 A CN 200710153837A CN 101117585 B CN101117585 B CN 101117585B
- Authority
- CN
- China
- Prior art keywords
- waste plastic
- reactor
- oil
- temperature
- mineral oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to an oil refining technology by utilizing waste plastic, in particular to an industrialized fuel oil producing method by utilizing the waste plastic. The present invention solves the shortcoming existed in the prior art that the effect for using the waste plastic to produce the fuel oil is bad. The steps includes: dehydrated mineral oil is used as the medium of liquidized waste plastic to be put into a reactor, the mineral oil being used for liquidizing the waste plastic is preheated in the reactor, the waste plastic is put into the reactor, the waste plastic in the reactor is stably heated and time-lapsed cracked, gaseous hydrocarbon produced from the reaction is fed into a flash distillation column, light distillated oil produced from the flash distillation column is distilled in the normal atmosphere. The present invention adopts molten salt as the heat-conducting medium, so as to enable the plastic being heated evenly, the operation temperature is controlled at 500 DEG C, the liquid liquidoid temperature inside the reactor is controlled at 370 DEG C for delaying the cracking operation and stabilizing the cracking temperature, the liquid inside the reactor is cracked under the stable condition, so as to overcome disadvantages in the prior art that using the coal fire to burn directly, the stability of the oil product is bad and the yield of the liquid is low.
Description
Technical field
The present invention relates to a kind of waste plastic lard oil technology of utilizing, be specially oil fuel is produced in a kind of industrialization with waste plastic method.
Background technology
From the seventies in last century so far, the a lot of researchers in the whole world have been paid a large amount of human and material resources and have been engaged in the research of producing oil fuel with waste plastic, only the patent documentation published of China just has about 200 parts, and consistently generally acknowledge that producing oil fuel with waste plastic is a kind of method that reclaims waste plastic preferably, see that with regard to present disclosed patent documentation existing method with waste plastic oil refining is to have applied mechanically thermally splitting and the two kinds of technical schemes of catalytic cracking in the refining of petroleum substantially.As if these two kinds of technology transplant are to some reason on the waste plastic oil refining process theoretically, but through facts have proved, lacking these two technology of rigid transplanting under the certain condition, will make plastics oil refining step into mistaken ideas.As everyone knows, thermally splitting and catalytic cracking are mature technologies in the refining of petroleum field.The cracking of thermally splitting, catalytic cracking to as if liquid phase, by multiple hydro carbons and molecular weight hydrocarbon polymer not of uniform size, on the contrary, though plastics are the hydrocarbon polymers that become through polymerization process by hydrocarbon polymer, molecular weight is more than ten thousand grades, but it is the solid phase, and well-known thermocracking process is that the cracking object must be a liquid after the heating under certain temperature condition.Heating power disconnects in the formation molecular chain of the hydrocarbon polymer of macromolecule or little molecule thereupon; Catalytic cracking is catalytic activity and an adsorptive power of utilizing catalyst themselves with chemical mode, with oil and oil gas molecular adsorption, behind chemical reaction with cracked oil, gas molecule desorption, but precondition also is a heating back liquid hydrocarbon, in view of this, be the condition of carrying earlier of cracking technology with the phase transformation of plastics oil refining solid, liquid.Do not have thermally splitting with regard to seeing among present disclosed patent documentation and the embodiment, the plastics liquefaction measure before the catalytic cracking, most of embodiment utilizes extrusion machine that it is pushed into waste plastic to add thermally splitting in the reactor, or catalyzer is put into by a certain percentage carried out catalytic cracking in the reactor simultaneously, as everyone knows, the plastics poor thermal conductivity, has the liquefaction property that absorbs heat gradually, even liquefaction back liquid is not that the image-stone petroleum hydrocarbon exists with the molecule monomer that differs in size like that yet.It is not monomer that plastics after practical observation confirms liquefaction still can become solid once the environment that breaks away from heat, form monomer and need the long period, this characteristic has also determined the selection of cracking Technology, and just see among present disclosed patent documentation and the embodiment, nearly all be to improve the rigid cracking of cracking temperature, this method is similar to coal and does the slide technology, consequently plastics are as high temperature, just produce dehydrogenation carbonization condensation reaction, liquid yield is low, and it is low that full in the oil product closes hydrocarbon content, antioxidant capacity is poor, easily generate the solubility colloid, and black with peculiar smell, therefore with plastics liquefaction before the operation of waste plastic production oil fuel; How in service be to utilize waste plastic to produce two big key problem in technology of oil fuel according to the characteristics of liquids selective cracking process technology behind the plastics liquefaction.
Summary of the invention
The present invention to produce the existing defective of oil fuel and provides a kind of industrialization to produce the method for oil fuel with waste plastic with waste plastic in order to solve in the prior art.
The present invention is realized that by following technical scheme the method that a kind of industrialization is produced oil fuel with waste plastic may further comprise the steps:
(1), the medium of doing the liquefaction waste plastic of the mineral oil after the dehydration drops in the reactor,
(2), to do in the reactor liquefaction waste plastic mineral oil give heat,
(3), waste plastic is dropped in the reactor,
(4), to the stable heating time-delay of waste plastic in reactor cracking, the hydrocarbon gas that reaction generates is sent flashing tower to,
(5), air distillation is carried out in the flashing tower benzoline of producing.
Reactor has reciprocating type interlock agitator in being in the described step (1), adorns the reactor that fused salt is done the heat-conducting medium chuck outward, and the discarded mineral oil input amount after the dehydration is 3/5ths of a reactor liquid phase section still appearance.The mineral oil that uses be discarded mineral oil.
In the described step (2) mineral oil of doing the liquefaction waste plastic in the reactor is preheating to 250 ℃～300 ℃, the temperature of molten salt in the reacting kettle jacketing is 350 ℃～400 ℃.
The waste plastic input amount is 2/5ths of a liquid phase section still appearance in the described step (3).
In the described step (4), produce oil fuel with waste plastic and formally start after finishing 1,2,3 steps, long according to the waste plastic heat conductivility difference liquefaction back cracking time, characteristics such as the too high easy generation condensation reaction of temperature need stable heating, postpone the cracking time.
With produce 1, Number 2 fuel oil is example＜SH, control chuck temperature of molten salt is 500 ℃, liquidus temperature is 370 ℃ in the still, the hydrocarbon gas that reaction generates enters flashing tower, tower still temperature is 320 ℃, flashing tower does not go out product and only goes out the basic material that the lightweight slide divides oil to do atmospheric fractional tower, and the feeding unit of reactor is quantitatively sent into waste plastic in the reactor according to the produced quantity of hydrocarbon gas in the still simultaneously.
In the described step (5), the benzoline of being produced by flashing tower enters atmospheric fractional tower through the disposable vaporization of process furnace, wherein furnace outlet oil gas temperature is 320 ℃, and the atmospheric fractional tower cat head is produced petroleum naphtha, produces light-weight fuel oil at the bottom of 150 ℃ of towers of cutting temperature.
The advantage that the present invention compared with prior art has is as follows;
1, makes the liquefaction medium owing to before producing, drop into a certain proportion of discarded mineral oil, overcome prior art and utilized wall to generate the defective that hydrothermal solutionization is brought with waste plastic oil refining production equipment reactor.As everyone knows: first gordian technique with waste plastic oil refining is liquefaction, from thing mutually, plastics are that solid oil is a liquid, be to refine oil with waste plastic, the phase transformation of solid and liquid just appears, see with regard to present disclosed patent documentation, consistent waste plastic is put into extrusion machine fires xeothermic heat absorption the material---plastics that pass to that heating facilities device wall generates in the reactor, heat absorption liquefaction is the waste plastic person's character, yet itself has the characteristic of heat absorption liquefaction gradually again, temperature low it easily touch molten, high its easy carbonization of temperature.Facts have proved owing to adopt the discarded mineral oil of usefulness of the present invention to make discarded plastics liquefaction medium, rigidly xeothermicly converted to flexible damp and hotly that heat passagely convert the transmission of width of cloth line to by straight line, the endotherm area of plastics increases.Therefore waste plastic disposable liquefaction of comprehensive heat absorption in the temperature environment of flexibility has reduced carbonization phenomenon, liquid transformation efficiency height.
2, the present invention has adopted stable cracking temperature in waste plastic oil refining production operation, postpones the cracking time and then has guaranteed the stability of oil product and yield has overcome prior art and directly burns the low defective of being brought of oil stability difference liquid yield with coal fire.Fact proved, waste plastic liquefaction back is flowable liquid phase under certain temperature environment, when it breaks away from certain temperature environment, it has been transformed into this characteristic of solid again, it be not liquefaction after image petroleum hydrocarbon like that with monomer in reactor, its molecular structure is with dendritic and wire combination, be similar to spongy Peng Run body, Gu this needs the long cracking time, if temperature has fluctuation or higher when operation, plastics liquid just can generate the condensation reaction of dehydrogenation carbonization when pyrolytic cracking, the low stability difference of oil product transformation efficiency is black and with peculiar smell.
The present invention has adopted fused salt to do heat-conducting medium, it is heated evenly, service temperature is controlled at 500 ℃, the liquid liquidus temperature is controlled at 370 ℃ to postpone the cracking operation in the still, nonvoluntary lifting or reduction cracking temperature, liquid cracking under stable condition has overcome prior art directly to burn the oil stability that is brought with coal fire poor in the still, the defective that liquid yield is low.
Description of drawings
Fig. 1 is for realizing the device assembles figure of present method
1-reactor among the figure, 2-fused salt chuck, the reciprocating type agitator of 3-, 4-sedimentation cylinder, 5-motor, the 6-spiral pump, 7-flashing tower, 8-tower still, 9-condenser, 10-gasoline water separator, 11-mixing oil storage cylinder, 12-process furnace, 13-separation column, 14-condenser, 15-condenser
Embodiment
The invention will be further described below in conjunction with accompanying drawing,
The method that a kind of industrialization is produced oil fuel with waste plastic may further comprise the steps:
1, select for use discarded mineral oil＜automobile-used gear oil, the machine oil after the dehydration or produce after this unit flashing tower still oil do liquefaction waste plastic medium and reciprocating type interlock agitator 3 arranged in putting into, adorn fused salt outward and do in the reactor of fused salt chuck 2 of heat-conducting medium.3/5ths of the liquid phase section still appearance that discarded mineral oil input amount is a reactor.Compound interlock agitator 3 functions mainly are to stir and remove the inwall green coke.
2, the discarded mineral oil of putting in the reactor is fired preheating, the temperature of molten salt in the fused salt chuck 2 is 350 ℃-400 ℃, and the discarded mineral oil in the reactor is 250 ℃-300 ℃.
3, with waste plastic PE, PP, PS compound, put in the reactor with extrusion machine, input amount is 2/5ths of a reactor liquid phase section still appearance, starts reciprocating type interlock agitator 3 then, waste plastic and the discarded mineral oil that contains heat melting liquefaction gradually.
4, after finishing the 1.2.3. step, the formal startup with plastics-production oil fuel production equipment, to produce No. 1, Number 2 fuel oil is example＜SH 〉, temperature of molten salt in the fused salt chuck is 500 ℃, liquidus temperature in the reactor is 370 °, the hydrocarbon gas that reaction generates enters flashing tower 7, tower still 8 temperature are 320 ℃, this tower does not go out product and only goes out the basic material that lightweight fraction oil is done atmospheric fractional tower 13, the inlet amount of while reactor, according to the produced quantity of reactor hydrocarbon gas, waste plastic is quantitatively sent in the reactor.
5, start dreg removing system, this system is made up of motor 5, spiral pump 6, sedimentation cylinder 4, sedimentation cylinder 4 is connected with the slag-drip opening of reactor 1, utilize different substances under with a temperature environment condition, the principle that material density has nothing in common with each other, effectively separate under action of gravity, the temperature in the operational process in the sedimentation cylinder 4 remains on more than 350 ℃ stage sedimentation regular cinder-discharge.
6, the light ends oil of being produced by flashing tower 8 enters into after condenser 9 condensations in vapour, oil, the water separator 10, and the oil after the separation enters and mixes oil cylinder 11, and water is discharged from the bottom, and inflammable gas is done fuel the reactor burning is provided with fixed attention.The light ends oil of producing, enter atmospheric fractional tower through process furnace 12 disposable vaporizations, wherein process furnace 12 outlet oil gas temperature are 320 ℃, separation column ejects petroleum naphtha and enter the storage cylinder after condensation, No. 1, production or Number 2 fuel oil recovered temperature are 320 ℃ at the bottom of separation column 13 towers, enter the storage cylinder after condensation.
Claims (4)
1. the industrialization method of producing oil fuel with waste plastic is characterized in that: may further comprise the steps:
(1), the medium of doing the liquefaction waste plastic of the mineral oil after the dehydration drops in the reactor, described reactor has reciprocating type interlock agitator in being, adorns the reactor that fused salt is done the heat-conducting medium chuck outward,
(2), the mineral oil of doing the liquefaction waste plastic in the reactor is preheating to 250 ℃～300 ℃, the temperature of molten salt in the reacting kettle jacketing is 350 ℃～400 ℃,
(3), waste plastic is dropped in the reactor,
(4), to the stable heating time-delay of waste plastic in reactor cracking, the hydrocarbon gas that reaction generates is sent flashing tower to, control chuck temperature of molten salt is 500 ℃, liquidus temperature is 370 ℃ in the still, the hydrocarbon gas that reaction generates enters flashing tower, tower still temperature is 320 ℃,
(5), the benzoline of being produced by flashing tower enters atmospheric fractional tower through the disposable vaporization of process furnace, wherein furnace outlet oil gas temperature is 320 ℃, the atmospheric fractional tower cat head is produced petroleum naphtha, and cutting temperature is 150 ℃, and producing the light-weight fuel oil recovered temperature at the bottom of the fractionation Tata is 320 ℃.
2. the method that industrialization according to claim 1 is produced oil fuel with waste plastic is characterized in that: the mineral oil input amount in the step (1) after the dehydration is 3/5ths of a reactor liquid phase section still appearance.
3. the method that industrialization according to claim 1 is produced oil fuel with waste plastic is characterized in that: the waste plastic input amount is 2/5ths of a liquid phase section still appearance in the described step (3).
4. the method that industrialization according to claim 1 is produced oil fuel with waste plastic is characterized in that: institute's mineral oil that uses is to discard mineral oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200710153837XA CN101117585B (en) | 2007-09-13 | 2007-09-13 | Industrialized method for producing fuel oil by using waste plastics |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200710153837XA CN101117585B (en) | 2007-09-13 | 2007-09-13 | Industrialized method for producing fuel oil by using waste plastics |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101117585A CN101117585A (en) | 2008-02-06 |
| CN101117585B true CN101117585B (en) | 2010-11-10 |
Family
ID=39053847
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200710153837XA Expired - Fee Related CN101117585B (en) | 2007-09-13 | 2007-09-13 | Industrialized method for producing fuel oil by using waste plastics |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101117585B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746896B (en) * | 2011-04-22 | 2014-10-15 | 中国石油天然气股份有限公司 | Heating method and device of hydrogenation feed |
| CN102191107A (en) * | 2011-04-26 | 2011-09-21 | 杨波 | Process for carbonizing organic waste residues |
| ES2762959T3 (en) * | 2016-06-23 | 2020-05-26 | Suez Groupe | Procedure for the conversion of plastics into fuel |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1174873A (en) * | 1997-08-25 | 1998-03-04 | 廖蕴真 | Method for making petroleum products from waste plastics |
| CN1184537A (en) * | 1995-03-14 | 1998-06-10 | 自适应网络公司 | Method and apparatus for data encoding and communication over noisy media |
| CN1266879A (en) * | 1999-03-13 | 2000-09-20 | 张洪孝 | Process for producing fuel oil from waste or used plastics |
-
2007
- 2007-09-13 CN CN200710153837XA patent/CN101117585B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1184537A (en) * | 1995-03-14 | 1998-06-10 | 自适应网络公司 | Method and apparatus for data encoding and communication over noisy media |
| CN1174873A (en) * | 1997-08-25 | 1998-03-04 | 廖蕴真 | Method for making petroleum products from waste plastics |
| CN1266879A (en) * | 1999-03-13 | 2000-09-20 | 张洪孝 | Process for producing fuel oil from waste or used plastics |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101117585A (en) | 2008-02-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Ayoob et al. | Biodiesel production through transesterification of a mixture of non-edible oils over lithium supported on activated carbon derived from scrap tires | |
| Zhang et al. | Microwave-enhanced pyrolysis of natural algae from water blooms | |
| US20110011721A1 (en) | Vacuum Pyrolytic Gasification And Liquefaction To Produce Liquid And Gaseous Fuels From Biomass | |
| CN102154044B (en) | Method for preparing engine fuel gas by using biomass and/or organic waste | |
| WO1997019146A1 (en) | Process and apparatus for treatment of waste plastic hydrocarbons | |
| CN107746722A (en) | The method and apparatus that a kind of cracking waste plastics prepare gasoline and diesel oil | |
| CN106520176B (en) | A method of with polyolefin plastics preparing small molecule alkene | |
| CN101294091B (en) | Method and equipment for extracting gasoline diesel oil from oil-containing plants | |
| EP1707614A1 (en) | Thermal or catalytic cracking process for hydrocarbon feedstocks and corresponding system | |
| CN101457149B (en) | Method for producing gasoline and diesel oil by lipid | |
| CN1397627A (en) | Process and equipment for preparing gasoline and diesel oil from waste plastics and/or heavy oil | |
| CN101117585B (en) | Industrialized method for producing fuel oil by using waste plastics | |
| CN103723728A (en) | Activated carbon and method for preparing activated carbon from coal-directly liquefied residue | |
| CN202576344U (en) | Equipment for extracting oil fuel from sandy oil sludge or/and organic waste | |
| CN105505429A (en) | Oil preparation and gas production system and technology by conducting pressurization, hydrogenation and pyrolysis on large-sized seaweeds | |
| CN106811226B (en) | The device and method of biomass dual temperature section catalytic pyrolysis preparation high-quality liquid fuel | |
| CN108342211A (en) | A kind of novel biomass pyrolysis comprehensive utilization process and system | |
| CN114790397A (en) | Method for preparing electrode material by polymerizing and modifying biomass pyrolysis oil | |
| TW201502174A (en) | System and method for converting plastic/rubber to hydrocarbon fuel by thermo-catalytic process | |
| CN109337703A (en) | A kind of biomass continous way is catalyzed preparation high-quality oil-gas integrating device online | |
| CN1208430C (en) | Oil refining procss from waste plastic and equipment | |
| CN201053008Y (en) | Device for catalyzing biomass fast thermal cracking by high temperature ironic liquid | |
| CN101613613B (en) | Efficient heat energy utilization method used during fast thermal cracking of straw | |
| EP3312223B1 (en) | Method for thermally decomposing polyethylene and polypropylene waste | |
| CN107057744A (en) | The equipment and technique of a kind of formula of being slagged tap after continuity auger environmental protection oil refining |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP02 | Change in the address of a patent holder |
Address after: 100081 Beijing city Haidian District Sijiqing cottage Chapeng No. 73 Patentee after: Dang Derun Address before: 034000, Shanxi City, Xinzhou Province Long West Street, No. 13, city science and Technology Bureau He Huanliang turn Patentee before: Dang Derun |
|
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20101110 Termination date: 20120913 |